US8084639B2 - Method of reducing inflow of water from a reactor outlet gas to a dehydration tower for separating carboxylic acid solvent and water - Google Patents

Method of reducing inflow of water from a reactor outlet gas to a dehydration tower for separating carboxylic acid solvent and water Download PDF

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Publication number
US8084639B2
US8084639B2 US11/916,267 US91626707A US8084639B2 US 8084639 B2 US8084639 B2 US 8084639B2 US 91626707 A US91626707 A US 91626707A US 8084639 B2 US8084639 B2 US 8084639B2
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water
xylene
absorption tower
aromatic compound
reactor outlet
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US11/916,267
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US20090326264A1 (en
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Ki Joon Kang
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Amtpacific Co Ltd
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Amtpacific Co Ltd
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
    • C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
    • C07C51/255—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting
    • C07C51/265—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting having alkyl side chains which are oxidised to carboxyl groups
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F24—HEATING; RANGES; VENTILATING
    • F24F—AIR-CONDITIONING; AIR-HUMIDIFICATION; VENTILATION; USE OF AIR CURRENTS FOR SCREENING
    • F24F13/00—Details common to, or for air-conditioning, air-humidification, ventilation or use of air currents for screening
    • F24F13/02—Ducting arrangements
    • F24F13/0254—Ducting arrangements characterised by their mounting means, e.g. supports
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1487—Removing organic compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1493—Selection of liquid materials for use as absorbents
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/42—Separation; Purification; Stabilisation; Use of additives
    • C07C51/47—Separation; Purification; Stabilisation; Use of additives by solid-liquid treatment; by chemisorption
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F24—HEATING; RANGES; VENTILATING
    • F24F—AIR-CONDITIONING; AIR-HUMIDIFICATION; VENTILATION; USE OF AIR CURRENTS FOR SCREENING
    • F24F7/00—Ventilation
    • F24F7/04—Ventilation with ducting systems, e.g. by double walls; with natural circulation
    • F24F7/06—Ventilation with ducting systems, e.g. by double walls; with natural circulation with forced air circulation, e.g. by fan positioning of a ventilator in or against a conduit
    • F24F7/10—Ventilation with ducting systems, e.g. by double walls; with natural circulation with forced air circulation, e.g. by fan positioning of a ventilator in or against a conduit with air supply, or exhaust, through perforated wall, floor or ceiling
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/80—Water

Definitions

  • the present invention relates to a method for reducing water from a reactor outlet gas in the oxidation process of aromatic compounds by passing the reactor outlet gas through a first absorption tower and a condenser. As the amount of water inflow into the dehydration tower decreases, the amount of the steam required to separate water and acetic acid is reduced and the load of the dehydration tower can be reduced.
  • the process of preparing terephthalic acid comprises an oxidation step of oxidizing p-xylene with air in the presence of a catalyst such as cobalt, manganese and bromide and a distillation step of recovering the acetic acid solvent from the reactor and removing water.
  • a catalyst such as cobalt, manganese and bromide
  • a distillation step of recovering the acetic acid solvent from the reactor and removing water.
  • FIG. 1 illustrates the conventional process of collecting acetic acid through azeotropic distillation using an azeotropic agent.
  • the conventional apparatus for collecting acetic acid through azeotropic distillation using an azeotropic agent comprises a dehydration tower ( 1 ) for separating acetic acid from water through azeotropic distillation, a condenser ( 2 ) for condensing the outlet gas from the top of the dehydration tower ( 1 ), an organic-water separation tank ( 3 ) for separating the liquid organic materials passing through the condenser ( 2 ) from water, a heater ( 4 ) for supplying steam to the dehydration tower ( 1 ) and a heat exchanger ( 5 ) for cooling the acetic acid discharged at the bottom of the dehydration tower.
  • This conventional technology is advantageous in that, by adding an azeotropic agent to a mixture of water and acetic acid, the energy consumption by the dehydration tower ( 1 ) can be reduced since the resultant azeotrope boils at a temperature lower than the boiling point of water.
  • the reactor outlet gas formed during the preparation of terephthalic acid is hot, 180° C. or higher, and includes non-compressible gases, e.g., nitrogen, acetic acid, p-xylene and water.
  • non-compressible gases e.g., nitrogen, acetic acid, p-xylene and water.
  • the reactor outlet gas is passed through several heat exchangers containing cooling water for heat exchange in order to gradually lower the temperature of the reactor outlet gas. Condensed acetic acid and some of water are returned to the reactor and the remaining water is sent to the dehydration tower for discharging.
  • the gas that has passed through the final heat exchanger includes a small amount of acetic acid and p-xylene.
  • the gas is sent to a high-pressure absorption tower, where p-xylene is collected as entrained by acetic acid, acetic acid is collected as entrained by water and non-condensible gases including nitrogen are sent to a gas discharging unit and processed there.
  • the liquid mixture of acetic acid and water that has passed through the final heat exchanger and has been condensed is sent to the dehydration tower, where acetic acid is discharged at the bottom of the dehydration tower and water is discharged at the top of the dehydration tower.
  • the method of separating acetic acid from water by gradually lowering the temperature of the reactor outlet gas using several heat exchangers is advantageous in that steam can be generated from the hot reactor outlet gas, energy consumption is inevitable since water has to be removed from acetic acid at the dehydration tower using steam.
  • the present invention has been made to solve this problem and it is an object of the present invention to provide a method of reducing water from the reactor outlet gas in the oxidation process of aromatic compounds without further energy consumption.
  • the present invention provides a method of reducing water from the reactor outlet gas in the oxidation process of an aromatic compound, which comprises: flowing the reactor outlet gas into the bottom inlet of a first absorption tower in which tray or packing is equipped as a means for increasing the gas-liquid contact surface; supplying an aromatic compound at the top inlet of the first absorption tower in order to collect the carboxylic acid selected from the group consisting of acetic acid, propionic acid and acrylic acid, and included in the reactor outlet gas, and to recover it through the bottom outlet of the first absorption tower; and discharging the water included in the reactor outlet gas along with the aromatic compound through the top outlet of the first absorption tower, condensing the water and the aromatic compound using a condenser, separating the water from the aromatic compound using an organic-water separator and discharging the water as wastewater.
  • the aromatic compound or the aromatic compound and part of the water separated by the organic-water separator are recycled to the first absorption tower and the gas discharged from the organic-water separator is transferred to a second absorption tower.
  • the aromatic compound is selected from the group consisting of o-xylene, m-xylene, p-xylene, benzene and toluene.
  • p-xylene is used.
  • the mixture discharged at the first absorption tower can be recycled to the reactor for the oxidation of the aromatic compounds, without using special separation apparatus.
  • FIG. 1 illustrates the conventional process of collecting acetic acid through azeotropic distillation using an azeotropic agent.
  • FIG. 2 illustrates the process of reducing water from the reactor outlet gas in the oxidation process of terephthalic acid in accordance with an embodiment of the present invention.
  • the liquid mixture of acetic acid, p-xylene and water that is discharged at the bottom outlet of the first absorption tower is recycled to the reactor for further production of terephthalic acid.
  • the liquid mixture comprises, in general, 10-60 wt % of acetic acid, 10-60 wt % of p-xylene and 3-40 wt % of water.
  • terephthalic acid is prepared by air oxidation of p-xylene in the presence of a catalyst, as seen in the following Scheme 1. About 65 parts by weight of p-xylene is required to prepare 100 parts by weight of terephthalic acid.
  • the water included in the reactor outlet gas is discharged at the top outlet of the first absorption tower along with excess p-xylene.
  • the gas including p-xylene and water is condensed by the first heat exchanger into a stream of about 100° C., condensed by the second heat exchanger into a stream of about 40° C. and is transferred to the organic-water separation unit.
  • p-Xylene is separated from water and collected there and water is discharged as wastewater.
  • the gas discharged by the organic-water separator is a gas of about 40° C. or below and is transferred to the second absorption tower, which is a common high-pressure absorption tower, and processed there as in the conventional method.
  • the reactor outlet gas is flown into the first absorption tower directly or passing through several heat exchangers. For example, if the gas passes through 4 heat exchangers, the hot reactor outlet gas of 120-190° C. that has passed through the second and third heat exchangers is flown into the bottom inlet of the first absorption tower and water is removed from the reactor outlet gas as described above.
  • the amount of the reactor outlet gas flown into the bottom inlet of the first absorption tower by splitting is determined depending on the amount of water to be removed in the entire preparation process of terephthalic acid.
  • the amount of water to be removed in the entire preparation process of terephthalic acid is 21-22 parts by weight per 100 parts by weight of the produced terephthalic acid and is calculated from 2 (moles of water) ⁇ 18 (molecular weight of water)/166 (molecular weight of terephthalic acid) ⁇ 100 (amount of terephthalic acid).
  • the amount of the total reactor outlet gas is determined between 300 and 700 tons.
  • the means for increasing the gas-liquid contact surface is constructed in the form of trays or packings.
  • FIG. 2 illustrates the process of reducing water from the reactor outlet gas in the oxidation process of terephthalic acid in accordance with an embodiment of the present invention.
  • the apparatus for removing water during the preparation of terephthalic acid in accordance with an embodiment of the present invention comprises a reactor ( 100 ), a first absorption tower ( 110 ), a first heat exchanger ( 120 ), a second heat exchanger ( 130 ), an organic-water separator ( 140 ) and a second absorption tower ( 150 ).
  • the first absorption tower ( 110 ) may be equipped with a means for increasing the gas-liquid contact surface, which may be constructed in the form of trays or packings, but the present invention is not limited thereby.
  • the first heat exchanger ( 120 ) cools the hot gas discharged at the top outlet of the first absorption tower ( 110 ).
  • the first heat exchanger ( 120 ) may produce a low-temperature steam of about 100° C.
  • the second heat exchanger ( 130 ) condenses the gas that has passed through the first heat exchanger ( 120 ) and separates it into a liquid mixture of water and p-xylene and a nitrogen-containing gas.
  • p-xylene is separated by the organic-water separator and water is processed as wastewater through a pipe (L 7 ). And, the gaseous material is transferred to the second absorption tower ( 150 ), a common high-pressure absorption tower, and processed there.
  • a reactor outlet gas discharged from a reactor ( 100 ) for the preparation of terephthalic acid is flown into the bottom inlet of a first absorption tower ( 110 ) via a pipe (L 2 ) directly or passing through several heat exchangers.
  • the reactor outlet gas is cooled to 120° C. to 190° C. by a heat exchanger (not illustrated) before being flown into the first absorption tower ( 110 ).
  • the reactor outlet gas comprises nitrogen, acetic acid, water and a small amount of organic materials.
  • the reactor outlet gas comprises 60-95 wt % of nitrogen, 1-18 wt % of acetic acid, 2-36 wt % of water and a small amount organic material, which may be methyl acetate, p-xylene, etc.
  • the aromatic compound p-xylene is flown in via pipes (L 4 , L 10 ).
  • the amount of p-xylene is preferably 2-5 weight equivalents of the water to be removed. If the amount of p-xylene is outside this range, acetic acid may be discharged at the top of the absorption tower along with the gas, without being sufficiently collected or excess p-xylene may be discharged at the bottom of the absorption tower, thereby resulting in problems.
  • the pipe (L 4 ) is the one through which a stream from the organic-water separator ( 140 ) to be described later is flown.
  • the reactor outlet gas flown into the bottom inlet of the first absorption tower ( 110 ) rises to the top of the first absorption tower ( 110 ) and the p-xylene flown into the top inlet of the first absorption tower ( 110 ) descends to the bottom of the first absorption tower ( 110 ).
  • first absorption tower ( 110 ) Inside the first absorption tower ( 110 ) is equipped a means for increasing the gas-liquid contact area constructed in the form of trays or packings. Passing through the trays or packings, the reactor outlet gas contacts p-xylene, during which process acetic acid and some of water included in the reactor outlet gas is absorbed by p-xylene and condensed to be collected at the bottom of the first absorption tower ( 110 ).
  • p-xylene acts as the solvent that absorbs the acetic acid and water included in the reactor outlet gas and, therefore, it is possible to recycle the liquid mixture discharged at the bottom of the first absorption tower ( 110 ) to the reactor ( 100 ) for the preparation of terephthalic acid via the pipe (L 9 ), without the need of solvent removal.
  • the p-xylene included in the liquid mixture discharged at the bottom of the first absorption tower may be separated by an organic-water separator to recycle it to the top inlet of the first absorption tower ( 110 ).
  • the water that has not been condensed at the bottom of the first absorption tower ( 110 ) is discharged to the top outlet of the first absorption tower ( 110 ) along with excess p-xylene and is condensed by condensers ( 120 , 130 ), which may be heat exchangers.
  • condensers 120 , 130
  • p-xylene is separated from water and the water is processed as wastewater.
  • the gas discharged by the organic-water separator ( 140 ) which comprises nitrogen, acetic acid and p-xylene, is transferred to the second absorption tower ( 150 ), a conventional high-pressure absorption tower, and processed there.
  • a mixture comprising 50-90 wt % of nitrogen, 5-30 wt % of p-xylene, 2-15 wt % of water, 5-500 ppm of acetic acid and a small amount of organic materials is discharged from the top outlet of the first absorption tower ( 110 ) via a pipe (L 5 ).
  • the mixture is cooled while passing through the first heat exchanger ( 120 ).
  • the temperature of the mixture flown into the first heat exchanger ( 120 ) is about 110° C. to 180° C.
  • the temperature of the mixture that has been cooled while passing through the first heat exchanger ( 120 ) is about 100° C.
  • a low pressure steam may be generated.
  • the mixture that has passed through the second heat exchanger ( 130 ) is separated by the organic-water separator ( 140 ).
  • the organic-water separator ( 140 ) nitrogen, non-condensed p-xylene and a small amount of acetic acid are collected to the second absorption tower ( 150 ), which is a conventional high-pressure absorption tower, in gaseous state via a pipe (L 8 ) and water is transferred to a wastewater processing system via a pipe (L 7 ).
  • the second absorption tower ( 150 ) which is a conventional high-pressure absorption tower, in gaseous state via a pipe (L 8 ) and water is transferred to a wastewater processing system via a pipe (L 7 ).
  • the p-xylene separated by the organic-water separator ( 140 ) is recycled to the top of the first absorption tower ( 110 ) via the pipe (L 4 ).
  • some of water may be recycled to the first absorption tower ( 110 ) via another pipe in order to lower the concentration of the acetic acid that is discharged by the organic-water separator ( 140 ) along with water.
  • the amount of water to be removed at the dehydration tower is decreased because some of water is discharged at the top outlet of the first absorption tower ( 110 ). Therefore, the energy consumption by the dehydration tower is reduced.
  • the operation of the dehydration tower may be made unnecessary.
  • Inflow and outflow conditions at the first absorption tower are given in Table 1 below.
  • the absorption tower had an inner diameter of 40 mm and the means for increasing the gas-liquid contact area was constructed in the form of random packing with a height of 1.5 m.
  • PX stands for p-xylene and KGa for kg/cm 2 (absolute pressure).
  • the amount of water to be removed at the dehydration tower is reduced by 77.6 g/hr and the amount of steam to be used by the dehydration tower decreases.
  • the energy consumption and load of the dehydration tower decrease.
  • the method for reducing water from a reactor outlet gas in the oxidation process of aromatic compounds in accordance with the present invention decreases the amount of steam required to separate water and acetic acid at the dehydration tower and the load of the dehydration tower. Further, by carefully controlling the flow amount of the reactor outlet gas to the first absorption tower, the operation of the dehydration tower may be made unnecessary.

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  • Chemical & Material Sciences (AREA)
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  • Organic Chemistry (AREA)
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  • Chemical Kinetics & Catalysis (AREA)
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US11/916,267 2006-02-20 2007-02-15 Method of reducing inflow of water from a reactor outlet gas to a dehydration tower for separating carboxylic acid solvent and water Expired - Fee Related US8084639B2 (en)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
KR20060016331 2006-02-20
KR10-2006-0016331 2006-02-20
KR1020070005367A KR100794317B1 (ko) 2006-02-20 2007-01-17 방향족 화합물의 산화반응시 반응기 배출가스로부터 물을제거하는 방법
KR10-2007-0005367 2007-01-17
PCT/KR2007/000812 WO2007097543A1 (en) 2006-02-20 2007-02-15 Reducing method of water from reactor outlet gas in the oxidation process of aromatic compound

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US8084639B2 true US8084639B2 (en) 2011-12-27

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US (1) US8084639B2 (de)
EP (1) EP1986762B1 (de)
JP (1) JP5336198B2 (de)
KR (1) KR100794317B1 (de)
CN (1) CN101384332B (de)
AT (1) ATE525120T1 (de)
AU (1) AU2007218513B2 (de)
BR (1) BRPI0706820A2 (de)
CA (1) CA2642712C (de)
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CN101537299B (zh) * 2009-03-19 2011-12-28 绍兴远东石化有限公司 一种回收利用对苯二甲酸生产尾气中有机物的方法
KR101222730B1 (ko) * 2010-08-05 2013-01-15 삼성토탈 주식회사 증류탑으로부터의 저압 스팀 생산방법
KR101305594B1 (ko) * 2011-09-09 2013-09-09 삼성토탈 주식회사 폐열을 이용한 방향족 화합물의 분리공정에서의 에너지 절감방법
KR101264603B1 (ko) 2011-09-15 2013-05-24 강기준 에너지 기여 결합 증류를 이용한 방향족 화합물 산화반응시 반응기 배출물로부터 물을 분리하고 카르복실산을 회수하는 장치 및 방법
KR101435569B1 (ko) * 2014-01-28 2014-08-28 (주)에이엠티퍼시픽 방향족 카르복시산 제조시 초산 회수 방법
CN105498453B (zh) * 2015-12-04 2017-11-03 常德市雄鹰科技有限责任公司 一种三醋酸甘油酯生产过程中的废气处理工艺
CN110922323B (zh) * 2019-11-27 2024-07-02 天津东大化工集团有限公司 甲苯连续催化氧化生产苯甲酸热电耦合高效节能减排工艺
CN114057252B (zh) * 2021-12-07 2024-05-03 天华化工机械及自动化研究设计院有限公司 改善精对苯二甲酸装置脱水塔水质的系统及其方法

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1996011899A1 (en) 1994-10-14 1996-04-25 Amoco Corporation Process for preparing aromatic carboxylic acids with efficient energy recovery
US6143925A (en) * 1998-06-05 2000-11-07 Mitsui Chemicals, Inc. Process for producing aromatic carboxylic acid
US6153790A (en) 1998-12-01 2000-11-28 Shell Oil Company Method to produce aromatic dicarboxylic acids using cobalt and zirconium catalysts
JP2003137833A (ja) 2001-11-02 2003-05-14 Mitsubishi Chemicals Corp テレフタル酸の製造方法
US20080097118A1 (en) * 2005-03-21 2008-04-24 Bp Corporation North America Inc. Process and Apparatus for Manufacturing Aromatic Carboxylic Acids Including Pure Forms Thereof

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1599864A (de) * 1968-11-25 1970-07-20
JP2620820B2 (ja) * 1991-04-12 1997-06-18 アモコ・コーポレーション 還元して精製テレフタル酸を調製するのに適する粗製テレフタル酸の調製方法
JP3198711B2 (ja) * 1993-03-30 2001-08-13 三井化学株式会社 テレフタル酸の製造方法および装置
WO1996006065A1 (en) * 1994-08-23 1996-02-29 Imperial Chemical Industries Plc Dehydration of acetic acid by azeotropic distillation in the production of an aromatic acid
JPH11171826A (ja) * 1997-12-05 1999-06-29 Mitsubishi Chemical Corp 芳香族カルボン酸の製造方法
RU2163592C2 (ru) * 1998-04-30 2001-02-27 Открытое акционерное общество "Научно-исследовательский и проектный институт мономеров с опытным заводом" Способ получения изофталевой кислоты
JP2002326001A (ja) * 2001-02-27 2002-11-12 Mitsubishi Chemicals Corp 共沸蒸留方法
US20050256335A1 (en) * 2004-05-12 2005-11-17 Ovidiu Marin Providing gases to aromatic carboxylic acid manufacturing processes

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1996011899A1 (en) 1994-10-14 1996-04-25 Amoco Corporation Process for preparing aromatic carboxylic acids with efficient energy recovery
US6143925A (en) * 1998-06-05 2000-11-07 Mitsui Chemicals, Inc. Process for producing aromatic carboxylic acid
US6153790A (en) 1998-12-01 2000-11-28 Shell Oil Company Method to produce aromatic dicarboxylic acids using cobalt and zirconium catalysts
JP2003137833A (ja) 2001-11-02 2003-05-14 Mitsubishi Chemicals Corp テレフタル酸の製造方法
US20080097118A1 (en) * 2005-03-21 2008-04-24 Bp Corporation North America Inc. Process and Apparatus for Manufacturing Aromatic Carboxylic Acids Including Pure Forms Thereof

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RU2423171C2 (ru) 2011-07-10
KR100794317B1 (ko) 2008-01-11
AU2007218513B2 (en) 2010-03-18
KR20070083174A (ko) 2007-08-23
CA2642712A1 (en) 2007-08-30
JP2009527473A (ja) 2009-07-30
JP5336198B2 (ja) 2013-11-06
BRPI0706820A2 (pt) 2011-04-12
ATE525120T1 (de) 2011-10-15
CN101384332B (zh) 2011-11-23
EP1986762A4 (de) 2010-10-27
CA2642712C (en) 2011-11-29
US20090326264A1 (en) 2009-12-31
RU2008134730A (ru) 2010-03-27
EP1986762A1 (de) 2008-11-05
CN101384332A (zh) 2009-03-11
EP1986762B1 (de) 2011-09-21
WO2007097543A1 (en) 2007-08-30
AU2007218513A1 (en) 2007-08-30

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